US4107195A - Preparation of zeolite ZSM-35 - Google Patents

Preparation of zeolite ZSM-35 Download PDF

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Publication number
US4107195A
US4107195A US05/789,900 US78990077A US4107195A US 4107195 A US4107195 A US 4107195A US 78990077 A US78990077 A US 78990077A US 4107195 A US4107195 A US 4107195A
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United States
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sub
hydrogen
crystalline aluminosilicate
aluminosilicate zeolite
synthetic crystalline
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Expired - Lifetime
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US05/789,900
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English (en)
Inventor
Louis Deane Rollmann
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Mobil Oil AS
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Mobil Oil AS
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Priority to US05/789,900 priority Critical patent/US4107195A/en
Priority to NZ186956A priority patent/NZ186956A/xx
Priority to CA301,014A priority patent/CA1107709A/en
Priority to GB15188/78A priority patent/GB1586029A/en
Priority to AU35234/78A priority patent/AU513667B2/en
Priority to FR7811481A priority patent/FR2387909A1/fr
Priority to JP4672678A priority patent/JPS53144500A/ja
Priority to ZA00782293A priority patent/ZA782293B/xx
Priority to BE187029A priority patent/BE866271A/xx
Priority to NL7804288A priority patent/NL7804288A/xx
Priority to IT22608/78A priority patent/IT1094920B/it
Priority to DE19782817575 priority patent/DE2817575A1/de
Priority to US05/925,014 priority patent/US4146584A/en
Application granted granted Critical
Publication of US4107195A publication Critical patent/US4107195A/en
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Expired - Lifetime legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
    • C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
    • C01B39/44—Ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38
    • C01B39/445—Ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38 using at least one organic template directing agent
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/65—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38, as exemplified by patent documents US4046859, US4016245 and US4046859, respectively
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/80—Mixtures of different zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/36—Steaming
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/18—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the mordenite type
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S423/00—Chemistry of inorganic compounds
    • Y10S423/23—Ferrierite, e.g. SR-D ZSM-33

Definitions

  • This invention relates to a new and improved form of zeolite ZSM-35, to a new and useful improvement in synthesizing zeolite ZSM-35 and to use of the zeolite ZSM-35 prepared in accordance hereto as a catalyst for organic compound, e.g. hydrocarbon compound, conversion.
  • organic compound e.g. hydrocarbon compound
  • this invention relates to an improved method of preparing zeolite ZSM-35 whereby synthesis is facilitated and the zeolite product exhibits enhanced purity and catalytic activity when compared to conventionally synthesized zeolite ZSM-35.
  • Zeolite ZSM-35 and its conventional preparation are taught by U.S. Pat. No. 4,016,245, the disclosure of which is incorporated herein by reference. It has a distinctive X-ray diffraction pattern which identifies it from other known zeolites.
  • Applicant knows of no prior art methods for preparing zeolite ZSM-35 utilizing the present improved method.
  • An improved method for preparing an improved crystalline aluminosilicate zeolite ZSM-35 exhibiting enhanced purity, catalytic activity and aging properties comprises forming a reaction mixture containing sources of an alkali metal oxide, an organic nitrogen-containing oxide, an oxide of aluminum, an oxide of silicon and water and having a composition, in terms of mole ratios of oxides, falling within the following ranges:
  • reaction conditions required consist of heating the foregoing reaction mixture to a temperature of from about 90° F to about 400° F for a period of time of from about 3 hours to about 100 days.
  • a more preferred temperature range is from about 150° F to about 400° F with the amount of time at a temperature in such range being from about 6 hours to about 80 days.
  • the digestion of the gel particles is carried out until crystals form.
  • the solid product is separated from the reaction medium, as by cooling the whole to room temperature, filtering and water washing.
  • butanediamine especially 1,4-butanediamine when compared with other diamines such as ethylenediamine, propanediamine or pentanediamine, is believed due to its ability to function as a template in the nucleation and growth of ZSM-35 crystals.
  • the crystals of ZSM-35 prepared in accordance hereto exhibit a plate-like morphology previously unreported for ZSM-35 prepared in the conventional manner.
  • the conventionally prepared ZSM-35 tends to exhibit lath-shaped crystals whose pore channels parallel the long dimension. Morphology changes, by their influence on diffusion dimensions in a zeolite can significantly enhance catalytic activity and aging characteristics.
  • the composition for the synthesis of synthetic ZSM-35 can be prepared utilizing materials which can supply the appropriate oxide.
  • Such compositions include aluminates, alumina, silicates, silica hydrosol, silica gel, silicic acid and hydroxides.
  • each oxide component utilized in the reaction mixture for preparing ZSM-35 can be supplied by one or more essential reactants and they can be mixed together in any order.
  • any oxide can be supplied by an aqueous solution, sodium hydroxide or by an aqueous solution of a suitable silicate; the organic nitrogen-containing cation can be supplied by a compound of that cation, such as, for example, the hydroxide or a salt, as well as by the indicated amine.
  • the reaction mixture can be prepared either batchwise or continuously. Crystal size and crystallization time of the ZSM-35 composition will vary with the nature of the reaction mixture employed.
  • the ZSM-35 composition as prepared hereby has a characteristic X-ray diffraction pattern, the values of which are set forth in Table 1, hereinafter.
  • the ZSM-35 composition as prepared hereby can also be identified, in terms of mole ratios of oxides and in the anhydrous state, as follows:
  • R is butanediamine or an organic nitrogen-containing cation derived therefrom
  • M is an alkali metal cation and x is greater than 8, and is characterized by a specified X-ray powder diffraction pattern. It will be noticed that the ratio of R to Al 2 O 3 may exceed unity in this material due to the occlusion of excess organic species (R) within the zeolite pores.
  • ZSM-35 as hereby prepared can further be characterized by its sorptive capacity at 90° C, as will be hereinafter established.
  • the zeolite hereby prepared has a formula, in terms of mole ratios of oxides and in the anhydrous state, as follows:
  • R is butanediamine or an organic nitrogen-containing cation derived therefrom
  • M is an alkali metal, especially sodium and y is from greater than 8 to about 50.
  • the original alkali metal cations of the as synthesized ZSM-35 can be replaced in accordance with techniques well known in the art, at least in part, by ion exchange with other cations.
  • Preferred replacing cations include metal ions, ammonium ions, hydrogen ions and mixtures thereof.
  • Particularly preferred cations are those which render the zeolite catalytically active especially for hydrocarbon conversion. These include hydrogen, rare earth metals, aluminum, metals of Groups IIA, IIIB IVB, VIB, VIII, IB, IIB, IIIA IVA.
  • the synthetic ZSM-35 zeolite prepared in accordance hereto possesses a definite distinguishing crystalline structure whose X-ray diffraction pattern shows substantially the significant lines set forth in Table 1.
  • the radiation was the K-alpha doublet of copper, and a scintillation counter spectrometer with a strip chart pen recorder was used.
  • Ion exchange of the sodium ion with cations reveals substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the silicon to aluminum ratio of the particular sample, as well as if it has previously been subjected to thermal treatment.
  • a further characteristic of ZSM-35 is its sorptive capacity proving said zeolite to have increased capacity for 2-methylpentane (with respect to n-hexane sorption by the ratio n-hexane/2-methylpentane) when compared with a hydrogen form of natural ferrierite resulting from calcination of an ammonium exchanged form.
  • the characteristic sorption ratio n-hexane/2-methylpentane for ZSM-35 (after calcination at 600° C) is less than 10, whereas that ratio for the natural ferrierite is substantially greater than 10, for example, as high as 34 or higher.
  • improved zeolite ZSM-35 may be used in a wide variety of organic compound, e.g. hydrocarbon compound, conversion reactions, it is notably useful in the processes of polymerization, aromatization and cracking.
  • Other conversion processes for which improved ZSM-35 may be utilized in one or more of its active forms include, for example, hydrocracking and converting light aliphatics to aromatics such as in U.S. Pat. No. 3,760,024.
  • Synthetic ZSM-35 zeolites prepared in accordance hereto can be used either in the organic nitrogen-containing and alkali metal containing form, the alkali metal form and hydrogen form or another univalent or multivalent cationic form. They can also be used in intimate combination with a hydrogenating component such as tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, or a noble metal such as platinum or palladium where a hydrogenation-dehydrogenation function is to be performed. Such components can be exchanged into the composition, impregnated therein or physically intimately admixed therewith.
  • Such components can be impregnated in or on to ZSM-35 such as, for example, by, in the case of platinum, treating the zeolite with a platinum metal-containing ion.
  • suitable platinum compounds for this purpose include chloroplatinic acid, platinous chloride and various compounds containing the platinum amine complex. Combinations of metals and methods for their introduction can also be used.
  • Synthetic ZSM-35 when employed either as an adsorbent or as a catalyst in a hydrocarbon conversion process, should be dehydrated at least partially. This can be done by heating to a temperature in the range of 200° C to 600° C in an inert atmosphere, such as air, nitrogen, etc. and at atmospheric or subatmospheric pressures for between 1 and 48 hours. Dehydration can also be performed at lower temperature merely by placing the catalyst in a vacuum, but a longer time is required to obtain a sufficient amount of dehydration.
  • Synthetic ZSM-35 prepared in accordance hereto can have the original cations associated therewith replaced by a wide variety of other cations according to techniques well known in the art.
  • Typical replacing cations include hydrogen, ammonium and metal cations including mixtures thereof.
  • replacing metallic cations particular preference is given to cations of metals such as rare earths, Mn, Ca, Mg, Zn, Cd, Pd, Ni, Cu, Ti, Al, Sn, Fe and Co.
  • Typical ion exchange techniques would be to contact the synthetic ZSM-35 zeolite with a salt of the desired replacing cation or cations.
  • a salt of the desired replacing cation or cations can be employed, particular preference is given to chlorides, nitrates and sulfates.
  • the zeolite is then preferably washed with water and dried at a temperature ranging from 150° F to about 600° F and thereafter may be calcined in air or other inert gas at temperatures ranging from about 500° F to 1500° F for periods of time ranging from 1 to 48 hours or more to produce a catalytically-active thermal decomposition product thereof.
  • the spatial arrangement of the aluminum, silicon and oxygen atoms which form the basic crystal lattices of ZSM-35 remains essentially unchanged by the described replacement of alkali metal as determined by taking an X-ray powder diffraction pattern of the ion-exchanged material.
  • the aluminosilicate prepared by the instant invention is formed in a wide variety of particle sizes.
  • the particles can be in the form of a powder, a granule, or a molded product, such as extrudate having particle size sufficient to pass through a 2 mesh (Tyler) screen and be retained on a 400 mesh (Tyler) screen.
  • the aluminosilicate can be extruded before drying or dried or partially dried and then extruded.
  • the ZSM-35 hereby prepared with another material resistant to the temperatures and other conditions employed in organic conversion processes.
  • matrix materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials such as clays, silica and/or metal oxides. The latter may be either naturally occurring or in the form of gelatinous precipitates, sols or gels including mixtures of silica and metal oxides.
  • Inactive materials suitably serve as diluents to control the amount of conversion in a given process so that products can be obtained economically and orderly without employing other means for controlling the rate or reaction.
  • zeolite materials have been incorporated into naturally occurring clays, e.g. bentonite and kaolin. These materials, i.e clays, oxides, etc., function, in part, as binders for the catalyst. It is desirably to provide a catalyst having good crush strength, because in a petroleum refinery the catalyst is often subjected to rough handling, which tends to break the catalyst down into powder-like materials which cause problems in processing.
  • Naturally occurring clays which can be composited with the hereby synthesized ASM-35 catalyst include the montmorillonite and kaolin family, which families include the sub-bentonites, and the kaolins commonly known as Dixie, McNamee, Georgia and Florida clays or others in which the main mineral constituents is halloysite, kaolinite, dickite, nacrite, or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification.
  • the ZSM-35 catalyst hereby synthesized can be composited with a porous matrix material such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia.
  • the matrix can be in the form of a cogel. A mixture of these components could also be used.
  • the relative proportions of finely divided crystalline aluminosilicate ZSM-35 and inorganic oxide gel matrix vary widely with the crystalline aluminosilicate content ranging from about 1 to about 90 percent by weight and more usually in the range of about 2 to about 50 percent by weight of the composite.
  • such charge stocks can be polymerized at temperatures between 550 550° 850° F at an hourly space velocity of between 0.5 and 50 WHSV and a pressure between 0.1 and 800 psig.
  • such stocks can be aromatized at temperatures between 800 and 1200° F and pressures from 1 to 10 atmospheres and space velocities between 0.1 and 10 WHSV.
  • a series of comparative experiments were conducted to study facility of crystallization at 100° C.
  • a reaction mixture was prepared, placed in a polypropylene jar and then a steam chest for crystallization.
  • the source of silicate was Q-Brand (27.8 wt. % SiO 2 , 8.4 wt. % Na 2 O and 63.8 wt. % H 2 O) and the source of aluminate was Al 2 (SO 4 ) 3 .16H 2 O in each instance.
  • conventional preparation technique was followed with the template being ethylenediamine or pyrrolidine.
  • a series of comparative experiments were conducted to study facility of crystallization at 160° C.
  • a reaction mixture was prepared, placed in a teflon jar and then a steam chest for crystallization.
  • the source of silicate was Q-Brand (27.8 wt. % SiO 2 , 8.4 wt. % Na 2 O and 63.8 wt. % H 2 O) and the source of aluminate was Al 2 (SO 4 ) 3 .16H 2 O in each instance.
  • conventional preparation technique was followed with the template being ethylenediamine or pyrrolidine.
  • Reaction conditions were 200 psig, hydrogen/hydrocarbon mole ratio of 4 and a weight hourly space velocity of about 4 hr -1 .
  • catalysts exhibit both their activity and their shape selectivity for paraffin conversion.
  • the catalysts may also effect a net alkylation of aromatics by the olefinic fragments of cracking, thereby increasing gasoline yield.
  • Reaction temperature and results are presented in Table 4. It is readily observed that the improved ZSM-35 (Example 19) prepared in accordance hereto was much more active, more selective and produced more gasoline-range yield (by aromatics alkylation) than the ZSM-35 samples prepared by conventional technique.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Inorganic Chemistry (AREA)
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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Silicates, Zeolites, And Molecular Sieves (AREA)
US05/789,900 1977-04-22 1977-04-22 Preparation of zeolite ZSM-35 Expired - Lifetime US4107195A (en)

Priority Applications (13)

Application Number Priority Date Filing Date Title
US05/789,900 US4107195A (en) 1977-04-22 1977-04-22 Preparation of zeolite ZSM-35
NZ186956A NZ186956A (en) 1977-04-22 1978-04-12 Synthetic crystalline aluminosilicate zeolite and catalytic conversion of organic compounds
CA301,014A CA1107709A (en) 1977-04-22 1978-04-12 Preparation of zeolite zsm-35
GB15188/78A GB1586029A (en) 1977-04-22 1978-04-18 Preparation of zeolite zsm-3k
FR7811481A FR2387909A1 (fr) 1977-04-22 1978-04-19 Zeolite a base d'aluminosilicate cristallin
AU35234/78A AU513667B2 (en) 1977-04-22 1978-04-19 Zeolite zsm 35
JP4672678A JPS53144500A (en) 1977-04-22 1978-04-21 Synthetic crystalline almino silicate* method of making same and contact converting process using same
ZA00782293A ZA782293B (en) 1977-04-22 1978-04-21 Preparation of zeolite zsm-35
BE187029A BE866271A (fr) 1977-04-22 1978-04-21 Zeolite a base d'aluminosilicate cristallin
NL7804288A NL7804288A (nl) 1977-04-22 1978-04-21 Synthetisch kristallijn aluminosilicaat-zeoliet, werk- wijze ter bereiding daarvan en werkwijze voor het kata- lytisch omzetten van organische verbindingen.
IT22608/78A IT1094920B (it) 1977-04-22 1978-04-21 Zeolite sintetica procedimento per la sua fabbricazione e suo impiego in procedimenti di conversione organica
DE19782817575 DE2817575A1 (de) 1977-04-22 1978-04-21 Synthetischer kristalliner aluminosilicat-zeolith, verfahren zu dessen herstellung und dessen verwendung
US05/925,014 US4146584A (en) 1977-04-22 1978-07-17 Catalytic conversion with zsm-35

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Application Number Priority Date Filing Date Title
US05/789,900 US4107195A (en) 1977-04-22 1977-04-22 Preparation of zeolite ZSM-35

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US05/925,014 Division US4146584A (en) 1977-04-22 1978-07-17 Catalytic conversion with zsm-35

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US (1) US4107195A (enrdf_load_stackoverflow)
JP (1) JPS53144500A (enrdf_load_stackoverflow)
AU (1) AU513667B2 (enrdf_load_stackoverflow)
BE (1) BE866271A (enrdf_load_stackoverflow)
CA (1) CA1107709A (enrdf_load_stackoverflow)
DE (1) DE2817575A1 (enrdf_load_stackoverflow)
FR (1) FR2387909A1 (enrdf_load_stackoverflow)
GB (1) GB1586029A (enrdf_load_stackoverflow)
IT (1) IT1094920B (enrdf_load_stackoverflow)
NL (1) NL7804288A (enrdf_load_stackoverflow)
NZ (1) NZ186956A (enrdf_load_stackoverflow)
ZA (1) ZA782293B (enrdf_load_stackoverflow)

Cited By (34)

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US4205052A (en) * 1979-02-01 1980-05-27 Mobil Oil Corporation Manufacture of synthetic mordenite
US4299732A (en) * 1978-10-06 1981-11-10 The British Petroleum Company Limited Process for the production of amorphous aluminosilicates and their use as catalysts
US4323481A (en) * 1981-02-26 1982-04-06 Standard Oil Company (Indiana) Synthesis of molecular sieves using beta-diketones as organic templates
US4349461A (en) * 1980-02-25 1982-09-14 Mobil Oil Corporation Group VIIA metal-modified zeolite catalysts
US4376104A (en) * 1979-01-05 1983-03-08 The British Petroleum Company Limited Method for preparing crystalline aluminosilicates
US4400328A (en) * 1981-10-19 1983-08-23 Yoshinobu Takegami Crystalline aluminosilicate zeolite catalyst and the method for manufacturing thereof
US4401637A (en) * 1980-02-21 1983-08-30 Basf Aktiengesellschaft Crystalline isotactic zeolites and their preparation
US4423021A (en) * 1979-08-08 1983-12-27 Mobil Oil Corporation Method of preparing silico-crystal ZSM-48
US4551321A (en) * 1980-06-07 1985-11-05 Laszlo Marosi Preparation of zeolites
US4721607A (en) * 1986-01-31 1988-01-26 Amoco Corporation Process for the production of boronaaronate molecular sieve using ethylenediamine and quinoline or isoquinoline
FR2607128A1 (fr) * 1986-11-21 1988-05-27 Inst Francais Du Petrole Nouvelles ferrierites, leur procede de preparation et leur utilisation
US4925548A (en) * 1989-07-13 1990-05-15 Mobil Oil Corp. Synthesis of crystalline ZSM-35 structure
US4970397A (en) * 1989-06-16 1990-11-13 Mobil Oil Corporation Method and apparatus for activating catalysts using electromagnetic radiation
US5053211A (en) * 1981-06-30 1991-10-01 Amoco Corporation Manufacture of AMS-18 crystalline borosilicate molecular sieve
US5174980A (en) * 1991-10-04 1992-12-29 Mobil Oil Corp. Synthesis of crystalline ZSM-35
US5190736A (en) * 1991-10-18 1993-03-02 Mobil Oil Corporation Synthesis of crystalline ZSM-35
US5288475A (en) * 1992-10-21 1994-02-22 Mobil Oil Corp. Synthesis of ZSM-35
US5985238A (en) * 1995-06-07 1999-11-16 Pq Corporation Process for preparing ferrierite
EP1314476A1 (en) * 2001-11-26 2003-05-28 Technische Universiteit Delft Zeolite catalysts and their use in selective catalytic reduction of NOx
US20090163757A1 (en) * 2007-12-20 2009-06-25 Gee Jeffery C Linear olefin isomer isomerization using molecular sieve catalysts
WO2012092436A1 (en) 2010-12-30 2012-07-05 Virent, Inc. Organo-catalytic biomass deconstruction
WO2012092440A1 (en) 2010-12-30 2012-07-05 Virent, Inc. Solvolysis of biomass using solvent from a bioreforming process
WO2012162403A1 (en) 2011-05-23 2012-11-29 Virent, Inc. Production of chemicals and fuels from biomass
WO2013077885A1 (en) 2011-11-23 2013-05-30 Virent, Inc. Dehydrogenation of alkanols to increase yield of aromatics
WO2014152370A2 (en) 2013-03-14 2014-09-25 Virent, Inc. Production of aromatics from di-and poly-oxygenates
WO2014190161A1 (en) 2013-05-22 2014-11-27 Virent, Inc. Process for converting biomass to aromatic hydrocarbons
WO2014190124A1 (en) 2013-05-22 2014-11-27 Virent, Inc. Hydrogenation of carboxylic acids to increase yield of aromatics
US9382185B2 (en) 2013-03-15 2016-07-05 Virent, Inc. Processes for converting biomass-derived feedstocks to chemicals and liquid fuels
WO2016179133A1 (en) 2015-05-05 2016-11-10 Shell Oil Company Reduced emissions aromatics-containing jet fuels
WO2017112716A1 (en) 2015-12-21 2017-06-29 Shell Oil Company Methods of providing higher quality liquid kerosene based-propulsion fuels
US11180376B1 (en) 2021-03-19 2021-11-23 Chevron U.S.A. Inc. Synthesis of zeolites having the ferrierite structure
WO2023064565A2 (en) 2021-10-14 2023-04-20 Virent, Inc. Systems and methods for reforming a heavy aromatic stream
WO2023064483A2 (en) 2021-10-14 2023-04-20 Virent, Inc. Systems and methods for producing high purity aromatics from a mixed aromatic feed stream
FR3142106A1 (fr) 2022-11-23 2024-05-24 IFP Energies Nouvelles Synthese d’une zeolithe izm-8 de type structural fer de haute purete

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US4139600A (en) * 1977-04-22 1979-02-13 Mobil Oil Corporation Synthesis of zeolite ZSM-5
CA1144137A (en) * 1979-12-26 1983-04-05 Donald A. Hickson Method for preparing crystalline zeolites
US4260843A (en) * 1980-02-25 1981-04-07 Mobil Oil Corporation Shape selective reactions with berylium-modified zeolite catalysts
US4275256A (en) * 1980-02-25 1981-06-23 Mobil Oil Corporation Shape selective reactions with group VIIA metal modified zeolite catalysts
US4259537A (en) * 1980-03-17 1981-03-31 Mobil Oil Corporation Shape selective reactions with group via modified zeolite catalysts
US4276437A (en) * 1980-05-23 1981-06-30 Mobil Oil Corporation Shape selective reactions involving zeolite catalyst modified with group IIIB metal
JPS577820A (en) * 1980-06-18 1982-01-16 Mitsubishi Heavy Ind Ltd Novel crystalline silicate and its manufacture
DE3037415A1 (de) * 1980-10-03 1982-05-27 Basf Ag, 6700 Ludwigshafen Verfahren zur herstellung eines zeoliths vom strukturtyp des ferrierit
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FR2607128A1 (fr) * 1986-11-21 1988-05-27 Inst Francais Du Petrole Nouvelles ferrierites, leur procede de preparation et leur utilisation
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FR3142106A1 (fr) 2022-11-23 2024-05-24 IFP Energies Nouvelles Synthese d’une zeolithe izm-8 de type structural fer de haute purete
WO2024110331A1 (fr) 2022-11-23 2024-05-30 IFP Energies Nouvelles Synthese d'une zeolithe izm-8 de type structural fer de haute purete

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JPS53144500A (en) 1978-12-15
NZ186956A (en) 1979-10-25
AU513667B2 (en) 1980-12-11
DE2817575C2 (enrdf_load_stackoverflow) 1989-10-12
IT1094920B (it) 1985-08-10
ZA782293B (en) 1979-12-27
FR2387909A1 (fr) 1978-11-17
CA1107709A (en) 1981-08-25
FR2387909B1 (enrdf_load_stackoverflow) 1982-10-01
GB1586029A (en) 1981-03-11
IT7822608A0 (it) 1978-04-21
AU3523478A (en) 1979-10-25
DE2817575A1 (de) 1978-10-26
NL7804288A (nl) 1978-10-24
BE866271A (fr) 1978-10-23

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